TimeDelay Systems: Modeling, Analysis, Estimation, Control, and Synchronization
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Fei Zhang, Shengyue Zong, Xiang Wang, Xiaohuai Ren, "An Expert PI Controller with Dead Time Compensation of Monitor AGC in Hot Strip Mill", Mathematical Problems in Engineering, vol. 2016, Article ID 3041538, 8 pages, 2016. https://doi.org/10.1155/2016/3041538
An Expert PI Controller with Dead Time Compensation of Monitor AGC in Hot Strip Mill
Abstract
Hot strip rolling production is a highspeed process which requires highspeed control and communication system, but because of the long distance between the delivery stand of the finishing mill and the gauge meter, dead time occurs when strip is transported from the site of the actuator to another location where the gauge meter takes its reading, which seriously affects the thickness control effect. According to the process model which is developed based on the measured data, a filtered Smith predictor is applied to predict the thickness deviation of the finishing mill. At the same time, an expert PI controller based on feature information is proposed for the strip thinning during looper rising and coiler biting period and the strip thickening during the tension loss period of the strip tail end. As a result, the thickness accuracy has been improved by about 1.06% at a steady rolling speed and about 1.23% in acceleration and deceleration.
1. Introduction
Figure 1 shows the outline of a typical 1700 mm hot strip mill (HSM). Its purpose is to process cast steel slabs into steel strip. Hot rolling can achieve large dimensional changes in a single step; the slabs, of up to 35 t weight, are typically 250 mm thick and 10 m long, and the rolled strips are typically 2 mm thick and 1250 m long. This reduction in thickness is achieved by passing the piece through a series of rolling mill stands. Typically, at the first stand, the roughing mill (RM), the thickness of the hot slab (1240°C) is reduced by making several passes, forward and reverse, through the mill. At the end of this roughing process the piece will be 35 mm thick and 70 m long and its temperature will have dropped to 1050°C. Further reduction in thickness takes place in the six or seven closecoupled rolling finishing stands. The strip elongation is so great that the piece can straddle a region from the finishing mill (FM) approach tables to the coiler. During this part of the process, pieces normally have a final rolling temperature of 870°C followed by coiling at 600°C [1].
Thickness precision is one of the most important quality indexes in strip rolling process [2, 3]. Monitor automatic gauge control (AGC) based on hydraulic roll gap control system is widely used in modern strip rolling mills [4–7]. In monitor AGC system, gauge meter is used to measure strip gauge derivation, which is installed at the delivery side of the finishing mill. The strip thickness can be controlled by adjusting the roll gap. Because of restriction of mill structure and requirement of maintenance, the install location of gauge meter is far from the mill. As shown in Figure 2, the rolling mill produces steel strip at a speed of , and gauge meter measures the strip thickness . By comparing with thickness reference , thickness deviation is obtained. Then the gap correction value of monitor AGC is calculated. At the same time, the gap correction value of other types of AGC is calculated too. and are subsequently added to the gap set value to get the target gap . At last, hydraulic cylinders are used to modify the gap between a pair of working rolls that squeeze the material into the desired thickness. The dead time in this process is caused by the distance between the rolls and the gauge meter
During that interval, the process does not respond to the controller’s activity at all, and any attempt to manipulate the process variable before the dead time has elapsed inevitably fails.
According to control theory, the time delay in any feedback system reduces system stability and deteriorates dynamic characteristics, especially for the case of , where is the time constant [8]. Because the inertia time constant of the hydraulic system is generally less than 50 ms, the value of of the delivery stand is greater than 0.5 and those of the upstream stands are much greater.
Plants with a long time delay can often not be controlled effectively using a simple PID (Proportional, Integral, and Derivative) controller. The main reason for this is that the additional phase lag contributed by the time delay tends to destabilize the closedloop system. The stability problem can be solved by decreasing the controller gain. However, in this case the response obtained is very sluggish [8, 9].
The Smith predictor (SP), shown in Figure 3, is well known as an effective dead time compensator for a stable process with long time delay [10]. The widespread application of the SP has been hindered by two problems. First, it is difficult to tune manually, because the practicing engineer is not very familiar with process modeling and it is a timeconsuming manual task. Second, the predictor is sensitive to process parameter variations, as in any other advanced control technique. Hence the need for retuning the SP is more frequent than that for the PID controller [11, 12].
2. Filtered Smith Predictor (FSP)
The wellknown SP is a dead time compensator (DTC) widely used in the industry in which a dead time nominal process model is used. Nevertheless, the main drawback of this algorithm is that dead time errors can destabilize the system. A robust solution is the FSP, in which a filter is included to attenuate the oscillation caused by delay mismatches [13]. The proposed controller is shown in Figure 4. It can be seen that the structure is the same as in the SP with an additional filter . Because of its characteristics, the FSP can be used to compute a controller taking into account the robustness, coping with unstable plants, improving the disturbance rejection properties, and decoupling the setpoint and disturbance responses [14]. Therefore, all the drawbacks of the SP are considered in the design, using only one structure and, as will be shown, a unified design procedure.
In the structure is a process model, is the dead timefree model and is the primary controller. In the nominal case the closedloop transfer function for setpoint changes is the same for the SP and FSP:
Note that the delay is eliminated from the characteristic equation and does not affect . Assume that the real plant differs from the nominal case and consider a family of plants such that , and its characteristic equation is given by
The condition for closedloop SP robustness is that, for all frequencies and all plants in the family, the distance between and the −1 point in the Nyquist diagram is greater than . Thus, for the SP, where is the imaginary unit and is the frequency, and is the multiplicative normbound uncertainty [15, 16].
Therefore, when the closedloop transfer equation (2) is defined, is also fixed and if is chosen for a high performance then robustness will be poor. Thus, if is not appropriately chosen, small uncertainties may destabilize the system.
The characteristic equation for is then
Considering that the nominal system is stable, the robust stability condition for the FSP is
If is a lowpass filter, it can be used to improve the robustness of the system at the desired region of frequency [14]. Although does not affect , it modifies the disturbance rejection response defined by
Thus must be tuned for a compromise between robustness and disturbance rejection performance.
Note that only and are modified by the inclusion of the filter. That is, the filter can be used to improve the robustness or the disturbance rejection capabilities of the system without affecting the nominal setpoint response. Furthermore, can be tuned to obtain an internal stable system when controlling unstable plants. Therefore, the proposed controller has enough degrees of freedom to obtain compromise between robustness and a desired setpoint and disturbance rejection responses.
3. FSP for Monitor AGC
A typical and basic modeling task is that associated with setting up the roll gaps in a mill. The large deformation force required to reduce the strip thickness from entry thickness to exit thickness causes the stand frame holding the rolls to stretch and mill rolls to bend and flatten. The result is the exit thickness as a function of force . In simplified form this can be expressed as [1]where is the unloaded roll gap and the term is the mill stretch.
As shown in Figure 5, the normally used simplified thickness model of gauge meter equation or spring equation has the following form [17]:where is the mill modulus or stiffness coefficient and is the approximate value of mill stretch.
Because of the inaccuracy of empirical formula and the measurement error, there is a deviation of the calculated thickness from the actual thickness. The delayed calculated thickness is compared with the measured thickness and the deviation of the two is obtained to correct the deviation and improve the model accuracy. The monitor AGC system with SP is shown in Figure 6, where is the calculated thickness and is the delayed calculated thickness.
As can be seen in Figure 6, the thickness deviation can be calculated by the following formula:
If the roll gap remains unchanged, we have [7]where refers to stand , and are the exit thickness and the entry thickness of stand , respectively, is the stiffness coefficient of stand , and is the plastics coefficient of the rolled material in stand .
Because the material flows passing through different stands are equal, the exit thickness of stand is equal to the entry thickness of stand with the dead time , which means thator
Substituting (12) in (10) we get
If the thickness deviation is relatively large, it will overload the delivery stand of the finishing mill and affect the crown and flatness of the strip, so Smith’s method monitor AGC correction is distributed to upstream stand AGC to prevent the load unbalance [7]. At the same time, because the first few stands are too far to get good control effect, monitor AGC is only implemented to the last three stands of the finishing mill, as shown in Figure 7, where is the exit thickness deviation to be eliminated; () are the distribution coefficients of stand and meet the condition of ; and () are the stiffness coefficients and plastic coefficients of stand ; , , and are the dead time when material is transported from F4 to F5, F5 to F6, and F6 to gauge meter, respectively; () are the thickness deviation to be eliminated by stand and its upstream stands; () are the thickness modification of stand influenced by thickness modification before stand ; () are the thickness deviation to be eliminated only by stand ; and () are the gap correction value of monitor AGC and other types of AGC of stand ; and are the gap set value and gap target value of stand ; represents the motor of looper.
As shown in Figure 7, the thickness deviation to be eliminated only by stand can be calculated from
4. Expert PI Controller Design
The ProportionalIntegral (PI) controller is adopted as the primary controller in monitor AGC. PI parameters and are expected to be modified appropriately based on the current status of the system to obtain a good dynamic performance in the actual control process. But the control algorithm purely based on the mathematical model is difficult to meet the requirements of the control system and get the satisfactory dynamic performance, especially in the case of parameter variations and load disturbances. The expert system adjusting control output based on feature information is proposed for the strip thinning during looper rising and coiler biting period and the strip thickening during the tension loss period of the strip tail end, as shown in Figure 8.
The expert PI controller is shown in Figure 9. The input basic information of the expert controller includes , , , , , , , and .
The main expert knowledge in the knowledge base is as follows:(1) and are 0.6 and 0.15, respectively, when the thickness set value is less than 2.0 mm, 0.8 and 0.2 when the value is 2.0 to 5.0 mm, and 1.1 and 0.22 when the value is greater than 5.0 mm;(2) and decrease 0.1 and 0.02, respectively, when the width set value is greater than 1450 mm;(3) decreases 0.2 and increases 0.04 during speedup rolling;(4) and increase 0.3 and 0.04, respectively, when SPCC steel is being rolled;(5) decreases 100 μm and 30 μm on the basis of during looper rising period and coiler biting period, respectively;(6) gradually increases on the basis of during tension loss period of the strip tail end;(7) reaches the preset maximum (or minimum) when is greater than 150 μm (or less than −150 μm);(8) increases 0.2 and decreases 0.02 when the absolute value of is greater than 100 μm and less than or equal to 150 μm;(9) decreases 0.2 and increases 0.02 when the absolute value of is greater than 10 μm and less than or equal to 50 μm;(10) is 0 and increases 0.04 when the absolute value of is less than 10 μm.
5. Application Results
The monitor AGC tactics have been applied to the thickness control of a 1700 mm HSM and achieved good control effect. The control quality and the robustness of the system are very good, which proves the rationality of the system control principle. The system overcomes the subjective phenomenon of the instability of the manual operation, reduces the labor intensity of the operator, and improves the quality of the steel strip. Figure 10 is a measurement by Xray gauge meter to the delivery thickness curve when the new monitor AGC system is working. As can be seen in Figure 8, the new AGC system achieves better thickness performance than the old AGC system.
We have collected statistics data for 2 months and conclude from the data analysis that the average thickness qualified rate of the AGC system with new monitor algorithm is generally higher than that of the AGC system with old algorithm. The application results of some main specifications are shown in Tables 1 and 2, where is the target thickness and is the thickness deviation. Taking the steel strip with mm as an example, the ratio in corresponding range μm at a steady rolling speed is calculated as follows:


It can be calculated from Tables 1 and 2 that the average ratio of the new system and the old system is 94.76% and 95.82% at a steady rolling speed and 94.27% and 93.04% in acceleration and deceleration. As an important indicator, the ratio in corresponding range is generally used to represent the thickness precision. Therefore, it can be said that the thickness accuracy has been improved by about 1.06% at a steady rolling speed and about 1.23% in acceleration and deceleration.
6. Conclusion
This paper has presented a monitor AGC algorithm of expert PI controller with FSP which is suitable for the control of processes with long dead time. Compared with a conventional algorithm it has the advantage of obtaining realtime thickness and improving robustness. Moreover, the discrete model of FSP control strategy is easy to implement and tune.
The disadvantage of new monitor AGC system is that the greater thickness deviation correction in downstream stands of FM causes the greater variation in strip shape quality resulting in excessive burden to the bending control system of work roll during thickness deviation correction, so the process automation system should adopt more accurate models and perform more exact setup calculations to overcome it.
Competing Interests
The authors declare that there are no competing interests regarding the publication of this paper.
Acknowledgments
This work is partially supported by the Fundamental Research Funds for the Central Universities (FRFTP15061A3), National Natural Science Funds of China (51404021), and Beijing Municipal Natural Science Foundation (3154035).
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Copyright © 2016 Fei Zhang et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.